EP2314370B1 - Mikrofluidische Vorrichtung für Reaktionen nicht mischbarer Flüssigkeiten - Google Patents

Mikrofluidische Vorrichtung für Reaktionen nicht mischbarer Flüssigkeiten Download PDF

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Publication number
EP2314370B1
EP2314370B1 EP11154021.7A EP11154021A EP2314370B1 EP 2314370 B1 EP2314370 B1 EP 2314370B1 EP 11154021 A EP11154021 A EP 11154021A EP 2314370 B1 EP2314370 B1 EP 2314370B1
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Prior art keywords
passage portion
passage
volume
initial
mixer
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English (en)
French (fr)
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EP2314370A3 (de
EP2314370A2 (de
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Bérengère Chevalier
Clemens Horn
Maxime Moreno
Pierre Woehl
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Corning Inc
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Corning Inc
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Priority claimed from EP07301042A external-priority patent/EP1992403B1/de
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Publication of EP2314370A3 publication Critical patent/EP2314370A3/de
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/421—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions by moving the components in a convoluted or labyrinthine path
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/433—Mixing tubes wherein the shape of the tube influences the mixing, e.g. mixing tubes with varying cross-section or provided with inwardly extending profiles
    • B01F25/4331—Mixers with bended, curved, coiled, wounded mixing tubes or comprising elements for bending the flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/30—Micromixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/30—Micromixers
    • B01F33/304—Micromixers the mixing being performed in a mixing chamber where the products are brought into contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
    • B01F33/811—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles in two or more consecutive, i.e. successive, mixing receptacles or being consecutively arranged
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2215/00—Auxiliary or complementary information in relation with mixing
    • B01F2215/04—Technical information in relation with mixing
    • B01F2215/0413—Numerical information
    • B01F2215/0418—Geometrical information
    • B01F2215/0431—Numerical size values, e.g. diameter of a hole or conduit, area, volume, length, width, or ratios thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/90—Heating or cooling systems
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors
    • B01J2219/00819—Materials of construction
    • B01J2219/00824—Ceramic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors
    • B01J2219/00819—Materials of construction
    • B01J2219/00831—Glass
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors
    • B01J2219/00851—Additional features
    • B01J2219/00858—Aspects relating to the size of the reactor
    • B01J2219/0086—Dimensions of the flow channels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors
    • B01J2219/00873—Heat exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors
    • B01J2219/00889—Mixing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors
    • B01J2219/0095—Control aspects
    • B01J2219/00984—Residence time

Definitions

  • the designed or preferred mode of operation is to react two reactant streams by flowing the entire volume of one reactant stream into inlet A shown in Figure 3 , while dividing the other reactant stream and flowing it into a first inlet B1 and multiple additional inlets B2. This allows the amount of heat generated in each mixer passage portion 30 to be reduced relative to the device of Figure 2 , and allows the stoichiometric balance of the reaction to be approached gradually from one side.
  • unitary devices in which the method may be performed are also disclosed.
  • Another such embodiment comprises a unitary thermally tempered microstructured fluidic device having a reactant passage therein with characteristic cross-sectional diameter in the 0.2 millimeter to 15 millimeter range, the passage having, in order along a length thereof: (1) two or more inlets for entry of reactants (2) an initial mixing passage portion characterized by having a form or structure that induces a degree of mixing and a first degree of pressure drop in fluids passing therethrough (3) an initial dwell time passage portion characterized by having a volume of at least 0.1 milliliter and a generally smooth and continuous form or structure that generally maximizes the available volume within the passage relative to the available volume within the device (4) one or more respective stabilizer passage portions, each stabilizer passage portion characterized by having a form or structure that induces a degree of mixing and a second degree of pressure drop in fluids passing therethrough, the second degree of pressure drop being less than the first degree, each stabilizer passage portion followed immediately by a corresponding respective additional dwell time passage portion.
  • Figure 3 is an alternative cross-sectional plan view of vertical wall structures within the volume 24 of Figure 1 ;
  • Figure 7 is a cross-sectional plan view of vertical wall structures within the volume 24 of Figure 1 according to another embodiment of a described device;
  • Figure 9 is a graph showing percentage yield as a function of number of stabilizers
  • Figures 11 and 12 are graphs showing theoretical numerical calculation of the effect of the number of mixing and/or mixing and stabilizer zones on radius of droplets and pressure drop for two different immiscible fluid pairs.
  • Figure 5 is a schematic diagram showing the flow of reactants according to the described methods as well as the generalized flow path within a unitary microstructured fluidic device 10 according to the present invention.
  • Two or more immiscible fluids comprising two or more reactants are fed into two or more inlets A and B to a reactant passage 26 within the unitary microstructured fluidic device 10.
  • the reactant passage desirably has characteristic cross-sectional diameter in the 0.2 millimeter to 15 millimeter range and has, in order along a length thereof, the two or more inlets A and B for entry of reactants, an initial mixer passage portion 38 characterized by having a form or structure that induces a degree of mixing in fluids passing therethrough, an initial dwell time passage portion 40 characterized by having a volume of at least 0.1 milliliter and a generally smooth and continuous form or structure that generally maximizes the available volume within the passage relative to the available volume within the device, and one or more additional mixer passage portions 44, each additional mixer passage portion followed immediately by a corresponding respective additional dwell time passage portion 46.
  • the additional mixer passage portion together with the associated corresponding additional dwell time passage portion 46 represent a unit 42 that is repeated n times, where n is a positive integer. Fluids exit the device 10 at outlet C.
  • unitary is understood herein a device that is structured and arranged such that the device is generally not understood to be capable of non-destructive disassembly.
  • Some examples include glass, glass-ceramic, and ceramic microstructured devices prepared according to the methods developed by the present inventors and/or their colleagues and disclosed for example in U.S. Patent No. 7,007,709, G. Guzman et al., 2006 . Such materials and methods are useful in the context of the present invention.
  • the method and the microstructured fluidic device represented by Figure 5 incorporate two important aspects of reaction in an immiscible fluid media, emulsification and reaction time.
  • the layout guarantees both high surface/volume ratio-provided by the initial mixer passage portion 38 and the one or more additional mixer passage portions 44-and significantly large internal volume-provided by the generally straight channels of the dwell time passage portions 40 and 46 between the spaced mixer zones.
  • the initial dwell time passage portion desirably has a volume of at least 0.1 milliliter, more desirably of at least 0.3 milliliter.
  • the one or more additional dwell time passage portions may desirably have about the same volume as the initial one, but it is not necessary that they all be the same volume.
  • Figure 6 is a cross section of wall structures useful in volume 24 of Figure 1 . Note that the structures of Figure 6 are intended for use with the structures shown in Figure 4 , resulting in increased dwell time passage volume in the same manner as discussed above for Figures 3 and 4 .
  • two or more immiscible fluids comprising two or more reactants are fed into two or more inlets A and B1 to a reactant passage 26 within the unitary microstructured fluidic device (a device 10 of the type shown generally in Figure 1 ).
  • the additional mixers 44 are structured so as to induce a lesser degree of pressure drop than the initial mixer passage portion 38. That is, additional mixer passage portions 44, assuming they are supplied with the same fluid at the same pressure and flow rate as the initial mixer passage portion 38, are structured and arranged so as to produce a lesser pressure drop than that produced by the initial mixer passage portion 38.
  • the additional mixers 44 are shorter than the initial mixer 38 and have fewer mixing elements 50 along their length.
  • the additional mixers serve in a sense more as stabilizers than mixers, and the usage of these stabilizers instead of full length mixers result in significantly reduced pressure drop for the reactant passage as a whole.
  • additional inlets B2 are not used, but are available for methods outside the scope of this invention.
  • Figure 7 is a cross-sectional plan view of vertical wall structures within the volume 24 of Figure 1 according to another embodiment of a device of the present invention. Note that, in the same manner as the structures of Figure 6 , the structures of Figure 7 are intended for use with the structures shown in Figure 4 , resulting in increased dwell time passage volume in the same manner as discussed above for Figures 3 and 4 .
  • no additional inlets are provided in the embodiment shown in Figure 7 .
  • the initial mixer 38 of this embodiment is in the form of a narrow, tortuous passage portion
  • the additional mixers or stabilizers 44 of this embodiment are in the form of chambers structured and configured so as to produce, at the flow rates useful in the structure, a self-sustaining oscillating jet.
  • the self-sustaining oscillating jet stabilizers 44 of Figure 7 generate even less pressure drop than the stabilizers 44 of Figure 6 , and maintain the emulsion almost as well.
  • the self-sustaining oscillating jet stabilizers 44 of Figure 7 are each configured in the form of chamber 60 having one (or optionally more separate) feed channel(s) 62, each of the one or more feed channels 62 entering the chamber 60 at a common wall 64 of the chamber 60, the one or more separate feed channels 62 having a total channel width 66 comprising the widths of the one or more separate channels 62 and all inter-channel walls, if any, taken together, the chamber 60 having a width 68 in a direction perpendicular to the one or more channels 62 of at least two times the total channel width 66.
  • the chamber 60 may also include one or more posts 70 that may serve to increase the pressure resistance of the otherwise relatively large open chamber.
  • test reaction An amidation reaction was used as test reaction.
  • the test procedure was the following: 1.682 g (0.01 mol) of 2-phenylacetic chloride (1) was dissolved in 1 L of dry ethyl acetate or toluene. 1-phenylethylamin (1.212 g, 0.01 mol) was dissolved in 1 L of 0.1 N sodium hydroxide solution. The two immiscible solutions were pumped with a constant ratio of 1:1 through the reactor with various flow rates at room temperature. The reaction was quenched at the exit of the reactor by collecting the liquids in a beaker containing a IN acid chloride solution. The organic phase was separated, dried and injected into a gas chromatograph for analysis.
  • Figure 10 shows the yield percentage as a function of the pressure drop in bar produced at various flow rates (not shown) for one comparative method/device (trace 48) and four applications of the described methods (traces 50-56).
  • the comparative device, trace 48 is the device of Figure 2 , having a single mixer passage portion and a single dwell time passage portion following.
  • the remaining traces 50-56 were all produced by methods including feeding all the reactants through multiple mixer passage portions each with an immediately following dwell time passage portion.
  • Trace 50 shows the yield results from the a device like that of Figure 3 , used as described in the described methods, while trace 52 shows results from the device of Figure 8 , with an added dwell time structure appended at the exit of the device.
  • the subsequent mixers have the same length and number of mixing elements as the initial mixer.
  • the traces 54 and 56 are from the device of Figure 7
  • trace 56 is from the device of Figure 6 .
  • Both trace 54 and 56 show the superiority of the preferred structures of the present invention in which the mixers or emulsifiers or stabilizers downstream of the initial mixer are shorter or otherwise less intensive (lower pressure drop) than the initial mixer. As shown in the traces 54 and 56, high yields at relatively low pressures were the result.
  • the optimal number N of total mixing and/or emulsification elements is considered as the variable for the analysis and calculated to find the trade-off between (i) pressure drop, (ii) total volume of the reactor to provide sufficient reaction time and (iii) the maximum diameter of the droplet in the dispersed phase of the emulsion.
  • the notations used are the following: ⁇ interfacial tension, ⁇ density of the mixture, S solubitity of the dispersed phase in the continuous medium, D diffusion coefficient, R gas molar constant, T temperature, V total volume of the reactor, V m volume of one emulsification element, V DT volume of one straight segment, ⁇ P m the pressure drop in one emulsification element, and Q total volumetric flowrate.
  • E m Q ⁇ ⁇ N ⁇ ⁇ ⁇ P m
  • the time of stability of the emulsion can be evaluated to give an order of magnitude for the desirable volume of the straight channels.
  • destabilization of the emulsion follows a maturing process (although other mechanisms could be envisaged, such as coalescence).
  • the radius of the droplet at the outlet of one emulsification element can be taken as d max / 2, if we want to minimize the size of the droplets in the reactor.
  • Figures 11 and 12 show the final results of this analysis on the simple model used to generate the data reported in this disclosure.
  • Figure 11 shows the results for Ethyl Acetate and water, wherein most of the droplet radius reduction has occurred by the fourth or fifth stabilizer.
  • Figure 12 shows that most of the droplet radius reduction occurs already after only one or two stabilizers. This shows that applying the principle of design described in this disclosure, an optimal can be found, and that the value of this optimal depends on the reaction.

Claims (6)

  1. Zusammenhängende thermisch angelassene mikrostrukturierte fluidische Vorrichtung (10), die darin einen Durchgang (26) für Reaktionssubstanzen mit einem charakteristischen Querschnittsdurchmesser im Bereich von 0,2 Millimetern bis 15 Millimetern umfaßt, der in der Reihenfolge entlang einer Länge desselben zwei oder mehr Einlässe (A, B) für den Einlauf der Reaktionssubstanzen, einen Anfangsmischerdurchgangsabschnitt (38), der eine Form oder Struktur aufweist, die ein Maß an Durchmischung und ein erstes Maß an Druckabfall in dadurch fließenden Fluiden induziert, einen Anfangsverweilzeitdurchgangsabschnitt (40), der ein Volumen von wenigstens 0,1 Millilitern und eine im allgemeinen glatte und durchgehende Form oder Struktur aufweist, die im allgemeinen das verfügbare Volumen im Durchgang (26) relativ zum verfügbaren Volumen in der Vorrichtung (10) maximiert, und wobei die Vorrichtung (10) ferner entlang des fluidischen Durchgangs (26) nach dem Anfangsverweilzeitdurchgangsabschnitt (40) einen oder mehrere entsprechende Stabilisatordurchgangsabschnitte (44) umfaßt, wobei jeder Stabilisatordurchgangsabschnitt (44) eine Form oder Struktur aufweist, die ein Maß an Durchmischung und ein zweites Maß an Druckabfall in dadurch fließenden Fluiden induziert, wobei das zweite Maß an Druckabfall geringer ist als das erste Maß, wobei auf jeden Stabilisatordurchgangsabschnitt (44) unmittelbar ein entsprechender jeweiliger Zusatzverweilzeitdurchgangsabschnitt (46) folgt,
  2. Mikrostrukturierte fluidische Vorrichtung (10) nach Anspruch 1, wobei der Anfangsverweilzeitdurchgangsabschnitt (40) dadurch gekennzeichnet ist, daß er ein Volumen von wenigstens 0,3 Millilitern aufweist.
  3. Mikrostrukturierte fluidische Vorrichtung (10) nach Anspruch 1 oder 2, wobei für den Durchgang (26) für Reaktionssubstanzen auf der Abstromseite des Anfangsmischerdurchgangsabschnitts (38) keine Einlässe vorgesehen sind.
  4. Mikrostrukturierte fluidische Vorrichtung (10) nach einem der Ansprüche 1 bis 3, wobei der Anfangsmischerdurchgangsabschnitt (38) einen engen gewundenen Durchgangsabschnitt umfaßt, der eine erste Länge aufweist, und der eine oder die mehreren Stabilisatordurchgangsabschnitte (44) jeweils einen engen gewundenen Durchgangsabschnitt aufweisen, der eine Länge aufweist, die kleiner ist als die erste Länge.
  5. Mikrostrukturierte fluidische Vorrichtung (10) nach einem der Ansprüche 1 bis 3, wobei der Anfangsmischerdurchgangsabschnitt (38) eine erste Anzahl von Mischerelementen (50) umfaßt und der eine oder die mehreren Stabilisatordurchgangsabschnitte (44) jeweils eine Anzahl von Mischerelementen (50) umfassen, die kleiner als die erste Anzahl ist.
  6. Mikrostrukturierte fluidische Vorrichtung (10) nach Anspruch 1 oder 2, wobei der Anfangsmischerdurchgangsabschnitt (38) einen engen gewundenen Durchgangsabschnitt umfaßt und wenigstens einer des einen oder der mehreren Stabilisatordurchgangsabschnitte (44) eine Strahlkammer mit selbsterhaltender Oszillation (60) umfaßt, die einen oder mehrere separate Zufuhrkanäle (62) aufweist, wobei jeder des einen oder der mehreren Kanäle (62) in die Kammer (60) an einer gemeinsamen Wand (64) der Kammer (60) einmündet, wobei der eine oder die mehreren separaten Kanäle (62) eine Gesamtkanalweite (66) aufweisen, die die Weiten des einen oder der mehreren separaten Kanäle (62) und alle Zwischenkanalwände, falls vorhanden, zusammen umfaßt, wobei die Kammer (60) eine Weite (68) in einer Richtung senkrecht zu dem einen oder den mehreren Kanälen (69) von wenigstens dem Doppelten der Gesamtkanalweite (66) aufweist.
EP11154021.7A 2007-05-15 2007-07-11 Mikrofluidische Vorrichtung für Reaktionen nicht mischbarer Flüssigkeiten Active EP2314370B1 (de)

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EP07301042A EP1992403B1 (de) 2007-05-15 2007-05-15 Mikrofluidische und selbstverzögernde oszillierende Mischer sowie Vorrichtungen und Verfahren zu deren Verwendung
EP11154021.7A EP2314370B1 (de) 2007-05-15 2007-07-11 Mikrofluidische Vorrichtung für Reaktionen nicht mischbarer Flüssigkeiten
EP07301224A EP1992404B1 (de) 2007-05-15 2007-07-11 Mikrofluidische Vorrichtung und Verfahren für Reaktionen nicht mischbarer Flüssigkeiten

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EP2314370A2 EP2314370A2 (de) 2011-04-27
EP2314370A3 EP2314370A3 (de) 2012-03-28
EP2314370B1 true EP2314370B1 (de) 2013-09-04

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US (1) US20100284240A1 (de)
EP (2) EP1992404B1 (de)
JP (1) JP2011509814A (de)
KR (1) KR20100034037A (de)
CN (1) CN101801512B (de)
TW (1) TW200918162A (de)
WO (1) WO2009009130A1 (de)

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WO2005072858A1 (en) 2004-01-26 2005-08-11 President And Fellows Of Harvard College Fluid delivery system and method
JP2008539090A (ja) * 2005-04-26 2008-11-13 アビザ テクノロジー リミティド マイクロ流体構造およびその製造方法
EP2216093A1 (de) 2009-01-30 2010-08-11 Corning Incorporated Bildung und in situ Abscheidung von Palladium, Pd(0), in Reaktoren
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EP2314370A3 (de) 2012-03-28
EP1992404A2 (de) 2008-11-19
KR20100034037A (ko) 2010-03-31
CN101801512B (zh) 2013-01-09
JP2011509814A (ja) 2011-03-31
CN101801512A (zh) 2010-08-11
US20100284240A1 (en) 2010-11-11
EP1992404B1 (de) 2011-03-23
EP2314370A2 (de) 2011-04-27
TW200918162A (en) 2009-05-01
EP1992404A3 (de) 2008-12-03

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